Process for cracking oil



Aug. 2, 1932. 1 KIRSCHBRAUN 1,870,178

PROCESS FOR CRACKINGOIL Original Filed Sept. 1G. 1920 2 Sheets-Sheet l Aug. 2, 1932.

L. KlRsczr-JlBRAUN- PROCESS FOR CRACKING OIL original Filed sept. 1o. 1920 2 Sheets-Sheet 2 Patented Aug. 2, 1932 .UNITED orties LESTER KIR-SCHBRAUN, OF LEONIA, NEW' JERSEY, ASSIGNOR T0 UNIVERSAL OIL .PRODUCTS COMPANY, OF CHICAGO, ILLINOIS, A CORPORATION OF SOUTH DAKOTA rnconss ron ennemis@ OIL Application filed September 10, 1920, Serial No. 409,389. Renewed May 28, 1928.

'5 like bodies from heavier ends of petroleum such as the gas oil or fuel oil cuts. rlhe object of the invention is to obtain a uniform distribution of the heat and pressure in the vapor chambers and a regulated discharge of the oil at various parts of an elongated vapor chamber. By injecting heated fresh oil into various parts of the vapor chamber, I will eliminate or greatly reduce the incrustation formation of carbon and tend to I sweep or carry the carbon out through the residuum line.

In the drawings:

Fig. 1 is a plan view, and Fig. 2 a side elevation of my apparatus.

Referring to the drawings in detail, 1 designates the furnace in which is supported the heating coil 2 which forms the cracking Zone. This coil may consist of 160 feet of four-inch pipe, and the inlet side of which is connected to a charging pump 3 leading to any suitable source of supply. Mounted in a suitable setting 4 is the vapor or reacting chamber 5, which may take the form of twelve-inch pipe. The hot oil passes through manifold line 6 and branches 7, 8, 9 and 10, to each of the tubes of the vapor chamber. A throttle valve 11 is interposed in each of the branches 7, 8, 9 and 10, whereby the amount of percentage of oil passing to any tube of the vapor chamber may be controlled at will. The residue is drawn off by line 12 controlled by valve 13 to any suitable receiver. A valve 14 is interposed at the entrance to the manifold 6. This valve is preferably left wide open, but may, if'desired, be more or less throttled to produce a differential pressure in the system.

The vapors pass out of the reacting chamber through risers 15, which are connected to an aerial condenser 16. yThe vapors which are condensed in the reflux condenser 16, pass back through lines 17 and 18 to the pump 3, where they are mixed with the fresh charging stock. The incondensible gas and uncondensed vapors pass to a water condenser 19 and thence to a receiver 20. This receiver 2O is provided with liquid draw-off line 21, controlled by valve 22 and gas draw-off 23 controlled by valve 24.

, 1n carrying out the process in the early part of the operation, of the oil may pass through the pipe 7, 15% through the pipe 8, 12% through the pipe 9, and 8% through pipe 10. 1n the latter part of the run 40% of the oil may pass through the pipe 7, 25% through pipe 8, 20%' through the pipe 9, and 15% through the pipe 10.

It is to be understood'that these percentages are merely illustrative and will vary with the character of the pressure distillate and end point gasoline desired, as well as the character of the charging stock. Starting with a gas oil of 32o Baume from a Kansas field, the oil temperature in the cracking Zone might be 7500 to 800 F., and the pressure 100 pounds. 65% of the oil might be converted vinto pressure distillate of 51O Baume gravity, yielding 35% of gasoline of 100 end point, this percentage being based on total charging stock.

As above stated, this run is merely illustrative of one manner of carrying out the invention. No hard and fast limits can be given for dierent kinds of oil being treated, and this, of course, varies still more where different end points, or different percentages of pressure distillate are desired.

1t is to be noted that the perforated pipes vwhich enter the reacting chamber into the various coils thereof are perforated throughout their length and are closed at their far ends so as to compel all of the oil to pass through the perforations. The oil should enter the perforated pipes while still in a liquid phase.

Particular advantages of this method of supplying oil to a vapor or reacting chamber reside in the fact that heat losses through conversion and vaporization of the lighter hydrocarbons are replenished by the introduction of adjusted quantities of heated oil from the heating zone at suitable intervals. rThe introduction of oil from the heating zone in one place necessitates an excess of heat in the cracking tubes in yorder to provide the yms heat necessary for conversion and vaporization and a consequent drop of temperature of the oil through the vaporizing tubes. As a result of this excessive heat, carbon is frequently produced in unusual quantities, in the latter. elements of the heating tubes. By the described method of introducing the hot oil, a mild degree of heat can be employed thereby eliminating difficulties attending this excessive heating in the cracking zone.

I claim as my invention:

1. A process of cracking oil, comprising passing oil through a heating zone, thence passing the same to a vaporizing zone containing a plurality of connected vaporizing tubes, in initially introducing different relative quantities of oil to each of said tubes, in varying the relative quantities of oil introduced to the tubes as the treatment proceeds, and in collecting and condensing the vapors from all of said tubes.

2. A process of cracking oil, comprising passing oil through a heating zone, thence passing the same to a vaporizing zone containingy a plurality of connected vaporizing tubes, in inititally introducing different relative quantities of oil to each of said tubes, in varying the relative quantities of oil introduced to the tubes as the treatment proceeds by decreasing the initial quantity introduced to one tube and increasing the initial quantity introduced to another tube and in condensino' and collecting the vapors from the plura ity of tubes.

LESTER KIRSCHBRAUN. 

